Quenching process for pyrolytically cracked hydrocarbons

ABSTRACT

Improved quenching of pyrolytically cracked gas is effected by separating the hydrocarbon-water emulsion produced in a quenching zone having a plurality of stages and then transferring the emulsion to the initial stage of the quenching zone wherein incoming gases vaporize the water from the emulsion. Also, transferring a slurry containing particulate carbon, e.g., produced in the Wulff process by scrubbing the exhaust gases of the generation step, to the initial stage of the quenching zone and recovery of hydrocarbon and particulate carbon is taught.

I United States Patent [1 1 3,674,890

Oleszko et al. July 4, 1972 541 QUENCHING PROCESS FOR 3,342,724 9/1967 Goering ..208/10l PYROLYTICALLY CRACKED 5 34 4/1941 Y ROC O 1,880,309 4/1928 1,938,991 12/1933 Wulff ..260/679 [72] Inventors: Thaddeus J. Oleszko, Neu Otting; Lynn P.

Walker, Burghausen, both of Germany Primary Examiner-Delbert E. Gantz Assistant Examiner.l. M. Nelson [73] Asslgnee' Marathon Company Findley Ohm Attorney-Joseph C. Herring, Richard C. Willson, Jr. and Jack [22] Filed: March 4, 1970 L. Hummel [21] Appl. No.: 16,443 [57] ABSTRACT lmproved quenching of pyrolytically cracked gas is effected g ggg egg ii 8 by separating the hydrocarbon-water emulsion produced in a [58] i 260/683 5g5/63 quenching zone having a plurality of stages and then transfer- 55/64 ring the emulsion to the initial stage of the quenching zone wherein incoming gases vaporize the water from the emulsion. Also, transferring a slurry containing particulate carbon, e.g., [56] References cued produced in the Wulff process by scrubbing the exhaust gases UNITED STATES PATENTS of the generation step, to the initial stage of the quenching zone and recovery of hydrocarbon and particulate carbon is 2,945,075 7/1960 Scofield ..260/679 taught 3,236,905 2/1966 Otsuka et al... ...260/679 2,928,886 3/1960 Nisbet et al ..260/683 22 Claims, 3 Drawing Figures r fi I 4A l I2 5 FDA 3 l 1 l5 i i 241 mi .1

BA V '14 PATENTEDJUL 4 m2 sum 2 or 5 Fig. 2

ATTORNEY QUENCHING PROCESS FOR PYROLYTICALLY CRACKED HYDROCARBONS BACKGROUND OF THE INVENTION The present invention relates to the process of thermal cracking of a hydrocarbon, more specifically to the quenching operation, and most specifically to the disposition of the oil and water emulsion and particulate carbon recovered in the quenching operation.

In the process of thermal cracking a hydrocarbon for the production of acetylene, ethylene, butadiene and other olefins, such as the Wulff process, finely divided carbon or soot particles are produced in the product gas. After the hydrocarbon has been cracked, the product gas is rapidly cooled or quenched to stop further reaction. The quenching operation is accomplished by contacting the hot product gas with a quenching liquid such as a hydrocarbon, e.g., oil, or water. An emulsion or slurry-emulsion is produced in the quenching operation. The slurry-emulsion consists of a hydrocarbon-water emulsion containing particles of finely divided carbon or soot. The emulsion or slurry-emulsion must be treated so as to recover the valuable materials therein to increase process efficiency and to avoid pollution problems.

In addition, the Wulff process is a regeneration process wherein a material such as ceramic tile is first heated by combustion gases and subsequently the heated tile is used to heat the hydrocarbon feed gas so as to produce a cracked gas product. The combustion gases produced in the heating portion of the regeneration cycle contain hydrocarbons and particulate carbon. To avoid air pollution problems and the fouling of equipment, the particulate carbon and hydrocarbons are scrubbed from the exhaust gases producing a slurry of scrubbing liquid, particulate carbon and hydrocarbons. The slurry must be treated so as to recover the valuable materials therein.

A number of patents have issued in the art. U.S. Pat. Nos. 2,394,849; 2,945,075; 2,982,794; and 3,236,905 all teach various quenching processes including hydrocarbon and water separation zones. None of the above patents teach the recycling of a hydrocarbon-water emulsion to the first stage of a quenching zone.

The object of this invention is to provide an economical process for treating hydrocarbon-water emulsions and/or slurries containing particulate carbon which are produced in the pyrolytic hydrocarbon cracking process. Thereby, efficiency of operation and pollution control are increased.

SUMMARY The present invention is a process for the treatment of hydrocarbon-water emulsions, particulate carbon-water slurries and particulate carbon-hydrocarbon slurries produced in a pyrolytic process for producing alkenes and alkynes. The process requires very little equipment and is economically feasible. It may be utilized with any pyrolytic process for the production of alkenes and alkynes.

BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a schematic process flow diagram for a two-stage quench process.

FIG. 2 is a schematic process flow diagram for a three-stage quench process.

FIG. 3 is a schematic process flow diagram for a scrubbing process for the exhaust gases produced in a regenerative pyrolytic hydrocarbon cracking process.

DESCRIPTION OF THE PREFERRED EMBODIMENTS The invention and its advantages may be more easily understood by reference to the drawings. FIG. 1 shows a twostage quench tower, which is the simplest embodiment of the present invention. In FIG. 1, high temperature cracked gas is introduced into the first stage of the quench tower 1 via line 2. Quenching oil is introduced into the first stage of the quench tower 1 via line 3. The cracked gas and the quenching oil is contacted in the first stage of the quench tower in countercurrent flow with the cracked gas passing through the stage separation device 4 into the final stage of the quench tower 5. Quenching oil remaining in the first stage of the quench tower l is withdrawn from the first stage via line 6. A portion of said withdrawn quenching oil is removed from the quench system via line 7. The remainder of said withdrawn quenching oil is recycled to the first stage of the quench tower 1 via line 3.

A final quenching liquid is introduced into the final stage of the quench tower 5 via line 9. The cracked gas and the final quenching liquid is contacted in countercurrent flow in the final stage of the quench tower 5 with the cracked gas passing from the quench tower to subsequent treatment via line 10. The liquid remaining in the final stage of the quench tower after the final quench liquid is contacted with the cracked gas is transferred from the final stage of the quench tower 5 to the separation zone 11 via line 12.

The liquid withdrawn from the final stage of the quench tower 5 ordinarily contains at least three phases. Said phases may be water, hydrocarbon or oil, and an emulsion of the water and the hydrocarbon oil. The purpose of the separation zone 11 is to separate the liquid withdrawn from the final stage of the quench tower 5 into the three separate phases. In FIG. 1, the water phase is withdrawn from the separation zone via line 13. The hydrocarbon phase or oil phase is withdrawn from the separation zone via line 14. In FIG. 1, a portion of the separated hydrocarbon phase or oil phase may be added, via dotted line 8, to that portion of the quench oil which is recycled in the first stage of the quench tower l. The separated hydrocarbon-water emulsion is transferred from the separation zone 11 to the first stage of the quench tower 1 via line 15.

The ordinary pyrolytic or thermal cracking process for cracking hydrocarbons to produce alkenes and alkynes also produce a substantial quantity of particulate carbon in the cracked gas product. Therefore, the cracked gas product entering the quenching process will ordinarily contain from about 0.001 to about 0.10 pounds of particulate carbon per pound of dry gas. In FIG. 1, the particulate carbon would be entering with the cracked gas via line 2. One of the purposes of the quenching process is to remove the particulate carbon from the cracked gas. Therefore, the quench oil leaving the first stage of the quench tower 1 via line 6 will ordinarily contain a substantial quantity of particulate carbon. A portion of the particulate carbon is removed from the quenching process entrained in that portion of said quench oil removed via line 7.

A portion of the particulate carbon may be carried by the cracked gas passing from the first stage of the quench tower 1 to the final stage of the quench tower 5. Therefore, particulate carbon is ordinarily entrained in the liquid which is transferred from the final stage of the quench tower to the separation zone. Consequently, the three liquid phases, which are separated in the separation zone 11, ordinarily contain particulate carbon. In addition, the particulate carbon collects preferentially in the emulsion phase of the liquid separated in the separation zone. One of the purposes of the present invention is to teach a process for the transfer of particulate carbon entrained in the hydrocarbon-water emulsion formed in the final stage of the quenching process to the quench oil of the first stage of the quenching process. The amount of particulate carbon entrained in the emulsion is from about 00001 to 0.10 pounds of carbon per pound of emulsion.

The preferred pressure within the quench tower or quenching zone is from about 0.1 to about 10 atmospheres; the more preferred pressure is from about 0.25 to about 5.0 atmospheres; and the most preferred pressure is from about 0.4 to about 3 atmospheres.

The preferred temperature of the cracked gas entering the quenching process is from about C. to about 800 C.; the more preferred temperature is from about 250 C. to about 600 C.; and the most preferred temperature is from about 350 C. to about 450 C.

The preferred temperature of the cracked gas passing from the first stage of the quenching zone 1 to the final stage of the quenching zone is from about C. to about 500 C.; the more preferred temperature is from about 50 C. to about 300 C.; and the most preferred temperature is from about 70 C. to about 170 C.

The preferred pressure within the separation zone above the liquid is from about 0.1 to about 10 atmospheres; the more preferred pressure is from about 0.25 to about 5.0 atmospheres; and the most preferred pressure is from about 0.4 to about 3 atmospheres. The preferred temperature of the separation zone is from about 10 C. to about 150 C.; the more preferred temperature is from about 25 C. to about 100 C.; and the most preferred temperature is from about 50 C. to about 90 C.

The quench oil utilized in the first stage of the quench zone is any hydrocarbon of which at least a portion is liquid at the operating temperatures and pressures of the quenching process. The quench oil may be a mixture of hydrocarbons, a portion of which may be a vapor at the operating temperatures and pressures. However, at least a portion of the quench oil is liquid at the operating temperatures and pressures so that polymeric organic compounds and particulate carbon are entrained in the quench oil and removed from the first stage of the quench zone via line 6.

The final quenching liquid utilized in the final stage of the quench zone 5 may be water, hydrocarbon or a mixture of hydrocarbon and water. The preferred temperature of the final quench liquid in line 9 is from about 5 C. to about 130 C.; the more preferred temperature is from about C. to about 80 C.; and the most preferred temperature is from about C. to about 50 C.

The preferred temperature of the cracked gas leaving the final stage of the quench zone 5 via line 10 is from about 15 C. to about 150 C.; the more preferred temperature is from about 20 C. to about 100 C.; and the most preferred temperature is from about C. to about 75 C.

If water is to be used as the final quench liquid, a portion of the water withdrawn from the separation zone via line 13 may be recycled to the final stage of the quench zone 5 by interconnecting line 13 and line 9. This is illustrated by dotted line 13A in FIG. 1. If necessary, the recycled water may be cooled in a cooling zone prior to introduction into the final stage of the quench zone 5 via dotted line 13A and line 7.

If a hydrocarbon is to be used as the final quench liquid in the final stage of the quench zone 5, a portion of the hydrocarbon phase removed from the separation zone via line 14 may be recycled to the final stage of the quench zone. This is shown by dotted line 8A interconnecting line 14 and line 9 in FIG. 1. If necessary, a portion of the separated hydrocarbon which is recycled to the final stage of the quench zone 5 may be cooled prior to introduction of the final stage via line 9.

The quench oil is recycled in the first stage quench zone 1 may be cooled in a cooling zone prior to introduction into the first stage of the quench zone via line 3.

The operating temperatures and pressures of the process are not critical. However, the temperature of the cracked gas within the first stage of the quench zone 1 must be maintained above the dew point for water. The dew point is a function of the concentration of water, the temperature of the cracked gas and the pressure within the quenching zone. It is detrimental to the process of this invention if water condenses and is entrained in the oil in contact with the cracked gas in the first stage of the quenching zone 1.

The equipment utilized to effect contact between the gaseous phase and the liquid phase in the quench stages of the quenching zone is not critical. Examples of equipment which may be used for this purpose are: bubble-cap trays, perforated plates, packed column, etc. The stage separation devices 4 and 4A may be any device which provides for the collection of a liquid and the passage of gas. An example ofsuch a device is the bubble-cap tray.

FIG. 2 illustrates the process of the present invention having a three-stage quenching zone. In FIGS. 1 and 2, like numbers denominate like parts of the process as illustrated by the Figures.

The distinction between the process shown in FIG. 2 and the process shown in FIG. 1 is that FIG. 2 has an intermediate quenching stage 16 within the quenching zone. An intermediate quench oil is introduced via line 17 into the intermediate quenching stage 16. The intermediate quench oil is contacted with the cracked gas in countercurrent flow. Cracked gas passes from the first stage of the quenching zone 1 through the stages separation device 4 into the intermediate stage of the quenching zone 16 and thence from the inter mediate stage of the quenching zone 16 through stage separation device 4A to the final stage of the quenching zone 5. The final stage of the quenching zone 5 shown in FIG. 2 is operated in the same manner as the final stage of the quenching zone shown in FIG. 1.

Intermediate quench oil is collected on stage separation device 4 and is withdrawn via line 17 and is recycled to the intermediate stage of the quenching zone 16. In the process, aromatic organic compounds produced in the cracking process tend to condense and collect in the intermediate stage of the quenching zone 16. The intermediate quench oil is ordinarily enriched in aromatic compounds. The volume of the intermediate quench oil is ordinarily increased. Therefore, a portion of the intermediate quench oil is removed from the quench process via line 18.

The preferred temperature of the cracked gas entering the quenching zone 16 is from about 15 C. to about 500 C.; the more preferred temperature is from about 50 C. to about 300 C.: and the most preferred temperature is from about 70 C. to about C. If necessary, the recycled intermediate quench oil may be cooled prior to introduction into the intermediate stage of the quench zone 16. Although the temperatures within the process having a three-stage quench zone are generally not critical, the intermediate stage of the quenching zone 16 and the first stage of the quenching zone 1 in FIG. 2, like the first stage of the quenching zone 1 in FIG. 1, must be maintained above the dew point for water. The dew point for water is a function of the pressure and temperature within the process and the concentration of water in the cracked gas. The temperature of the cracked gas leaving the intermediate stage must be maintained above the dew point for water.

The flow rates of the fluids within the process are interdependent upon the composition of the fluids, the physical properties of the fluids, and the desired operating conditions. The flow rates are not critical to the present invention except that water must not be allowed to condense in the quench oil in the first stage of the two-stage quenching process or in an intermediate stage of a quenching process having more than two stages.

The process utilized in the separation zone 11 of the quenching process is not critical. Examples of satisfactory processes are centrifugation and a gravity settling.

The conditions enumerated in the description of FIG. 1 also apply to like numbered parts of FIG. 2.

FIG. 3 illustrates the process wherein the exhaust gases produced in the heating phase of the regenerative pyrolytic cracking process, i.e., the Wulff process, are scrubbed to remove hydrocarbons and particulate carbon. In FIG. 3, the exhaust gases produced in the heating phase of the regeneration cycle are introduced into the scrubbing zone 19 via line 20. Scrubbing liquid is introduced into the scrubbing zone via line 21. Said scrubbing liquid may be either a hydrocarbon, water or a mixture of hydrocarbon and water. Scrubbed exhaust gas is withdrawn from the scrubbing zone via line 22. Scrubbing liquid is contacted with the exhaust gases in countercurrent flow. Scrubbing liquid containing hydrocarbons and particulate carbon produced in the heating phase of the regeneration cycle are collected and are removed from the scrubbing zone via line 23. Said scrubbing liquid cqntaining hydrocarbons and particulate carbon is transferred from the scrubbing zone to the first stage of the quench zone via line 23, as shown in FIG. 3, and via line 24 and line 15, as shown in FIGS. 1 and 2.

The operating temperature and pressure of the exhaust gas scrubbing zone are not critical. However, the scrubbing zone must be operated such that at least a portion of the scrubbing liquid remains as a liquid after contacting the exhaust gas. The flow rates, temperatures and pressures utilized in the scrubbing zone are a function of the engineering design and are not critical to the present invention.

As shown in FIGS. 1 and 2, the process of the present invention treats the hydrocarbon-water emulsion produced in the final or subsequent stage of the quench zone by first separating the hydrocarbon-water emulsion from the water phase and hydrocarbon phase and thence transferring the hydrocarbonwater emulsion to the first stage of the quench zone. The heat available in the cracked gas which enters the quenching process is utilized to vaporize substantially all of the water from the hydrocarbon. In this manner, the water is separated from the hydrocarbon.

If the hydrocarbon-water emulsion contains particulate carbon, the particulate carbon remains with the hydrocarbon in the first stage of the quench zone. Thus, the hydrocarbon and particulate carbon is separated from water.

Finally, the scrubbing liquid produced in the exhaust scrubbing process in a regenerative cracking process containing hydrocarbons and particulate carbon is treated in the first stage of the quench zone. If the scrubbing liquid introduced into the scrubbing tower is water, the water is separated from the hydrocarbons and particulate carbon. If the scrubbing liquid is a hydrocarbon, the hydrocarbon may be fractionated thereby concentrating the particulate carbon.

It is understood that the embodiments illustrated in the drawings do not limit this invention. The drawings merely illustrate the process of the present invention. Obvious modifications will be apparent to one skilled in the art upon reading the present invention. An example of such modifications is: the cocurrent contacting of the quench liquid with the cracked gas and the use of a separation zone following each stage of the quenching process. Such modifications are to be included within the spirit of the claims appended hereto.

The process of the present invention is illustrated in the following example:

EXAMPLE Five pounds of naphtha and pounds of steam are reacted per minute in a Wulff-type furnace producing a product having approximately 85 percent by dry weight of organic compounds having five or less carbon atoms, approximately 10 percent by dry weight of organic compounds having between six and carbon atoms and having 5 percent by dry weight of coke or particulate carbon based upon the weight of hydrocarbon feed. The cracked gas product containing the particulate carbon and the higher molecular weight organic compounds is introduced into the first stage of a quench tower at a temperature of about 430 C. The cracked gas product is contacted in countercurrent flow with quench oil having an initial temperature of about 95 C. The temperature of the quench oil is increased to about l60 C. after contacting the cracked gas product. The pressure of the quenching zone is about 0.5 atmospheres. The quench oil is subsequently removed from the first stage of the quench tower, with a portion of the quench oil being recycled through a cooling zone wherein the temperature of the quench oil is reduced from about 160 C. to about 95 C. The cracked gas product is passed from the first v stage of the quench tower to the intermediate stage of the quench tower. The temperature of the cracked gas passing from said first stage to the intermediate stage is about 150 C. The cracked gas product is contacted in the intermediate stage of the quench tower with a second quench oil in countercurrent flow. The initial temperature of the second quench oil or intermediate quench oil is about 80 C. The temperature of the intermediate quench oil is increased to about 140 C. while contacting the cracked gas product. The cracked gas product is then passed from the intermediate stage of the quench tower to the final stage of the quench tower wherein the cracked gas product is contacted with water in countercurrent flow. The temperature of the cracked gas product passing from the intermediate stage to the final stage of the quench tower is approximately C. The initial temperature of the quench water entering the final stage of the quench tower is approximately 30 C. The temperature of the quench water is increased to about 75 C. while contacting the cracked gas product. The cracked gas product is withdrawn from the final stage of the quench tower at a temperature of approximately 40 C. A liquid is collected at the bottom of the final stage of the quench tower having a mixture of a water phase, hydrocarbon phase, hydrocarbon-water emulsion phase and with particulate carbon entrained in the emulsion phase. The hydrocarbon-water emulsion phase is separated from the water phase and the hydrocarbon phase and is introduced into the first stage of the quench tower at a temperature of about 75 C. An oil phase is separated from the threephase mixture and a portion of the oil phase is utilized as makeup quench oil in the first stage of the quench tower. A portion of the water phase is cooled and utilized as quench water in the final stage of the quench tower. A portion of the quench oil removed from the first stage of the quench tower after contacting the cracked gas product is removed from the quenching process. Particulate carbon is thereby removed from the quenching process.

What is claimed is:

1. An improved process for quenching pyrolytically cracked gas at a temperature of about C. to about 800 C. and wherein the gas contains alkenes and alkynes having two or more carbon atoms comprising in combination cleaning and cooling the cracked gas in a quenching zone having a plurality of stages by first contacting the cracked gas with a quench oil in a first stage; contacting said cracked gas with a quenching liquid in a stage subsequent to said first stage; producing a liquid containing hydrocarbon, water, and a hydrocarbonwater emulsion in said subsequent stage; the improvement comprising withdrawing said liquid containing hydrocarbon, water, and hydrocarbon-water emulsion from said subsequent stage; transferring said liquid to a separation zone wherein said liquid is separated into a hydrocarbon phase, water phase, and a hydrocarbon-water emulsion phase; transferring said hydrocarbon-water emulsion phase to the first stage of the quenching zone; contacting said hydrocarbon-water emulsion phase with the cracked gas in the first stage at a point which is below the point at which the cracked gas is contacted with the quench oil at a sufficient temperature to substantially vaporize the water in the hydrocarbon-water emulsion; and maintaining the temperature, pressure, and water concentration within the first stage of the quenching zone such that substantially no water vapor condenses in the first stage of the quenching zone.

2. The process of claim I wherein the pyrolytically cracked gas contains from about 0.001 to about 0.10 pounds of particulate carbon per pound of dry gas.

3. The process of claim 1 wherein the pressure within the quenching zone is about 0.1 to about 10 atmospheres at the surface of the liquid.

4. The process of claim 2 wherein the hydrocarbon-water emulsion contains about 0.0001 to about 0.2000 pounds of particulate carbon per pound of emulsion.

5. The process of claim 1 wherein the pyrolytically cracked gas and the quench oil are contacted in countercurrent flow.

6. The process of claim 1 wherein at least a portion of the quench oil remains in a liquid phase in the first stage of the quenching zone.

7. The process of claim 6 wherein said remaining liquid quench oil is separated from the cracked gas after the quench oil contacts the cracked gas.

8. The process of claim 7 wherein at least a portion of the separated liquid quench oil is recycled into the first stage of the quenching zone.

9. The process of claim 7 wherein at least a portion of the separated liquid quench oil is cooled and then recycled to the first stage of the quenching zone.

10. The process of claim 7 wherein the separated liquid quench oil contains particulate carbon.

11. The process of claim 7 wherein at least a portion of the separated liquid oil is withdrawn from the quenching process thereby removing particulate carbon from the process.

12. The process of claim 1 wherein the temperature of the cracked gas passing from the first stage of the quenching zone to the stage subsequent to the first stage is about C. to about 500 C.

13. The process of claim 1 wherein the temperature within the separation zone is about 10 C. to about 150 C.

14. The process of claim 1 wherein the pressure within the separation zone is about 0.1 to about 10 atmospheres at the surface of the liquid.

15. The process of claim 1 wherein a portion of the hydrocarbon phase separated in the separation zone is transferred to the first stage of the quenching zone and is contacted with the pyrolytically cracked gas.

16. The process of claim 1 wherein a portion of the water phase separated in the separation zone is transferred to said subsequent stage and is contacted with the cracked gas.

17. In the regenerative pyrolytic hydrocarbon cracking process for producing acetylene, e.g., the Wulff process, wherein the exhaust gases produced in the generation step of the regeneration process containing particulate carbon and hydrocarbons are scrubbed with a scrubbing liquid to remove particulate carbon and wherein a slurry of particulate carbon, hydrocarbons and scrubbing liquid is produced and wherein the pyrolytically cracked gas containing acetylene is quenched in a quenching process having a plurality of stages, the first stage of which comprises contacting the cracked gas with a quench oil; the improvement comprising in combination transferring said slurry of particulate carbon and scrubbing liquid to the first stage of the quenching process and contacting said slurry with the cracked gas in the first stage of the quenching process at a point which is below the point at which the cracked gas is contacted with the quench oil, thereby vaporizing at least a part of the scrubbing liquid such that the particulate carbon may be entrained in the quench oil.

18. The process of claim 17 wherein the scrubbing liquid is water and wherein substantially all of the water is vaporized in the first stage of the quenching process.

19. The process of claim 17 wherein the scrubbing liquid is a hydrocarbon.

20. The process of claim 17 wherein the scrubbing liquid is a mixture of hydrocarbon and water and wherein substantially all of the water is vaporized in the first stage of the quenching process.

21. In a process for quenching pyrolytically cracked gas containing alkenes and alkynes having two or more carbon atoms and wherein the cracked gas is cleaned and cooled in a quenching zone; the improvement comprising in combination passing said cracked gas to a quenching zone having three stages; contacting said cracked gas with quench oil in countercurrent flow in a first stage; passing said cracked gas from said first stage to a second stage; contacting said cracked gas with a second quench oil in countercurrent flow in a second or intermediate stage; maintaining the temperature, pressure and water concentration in said first and intermediate stages such that substantially no water vapor is condensed in said first and intermediate stages; passing said cracked gas from said second stage to a final stage; contacting said cracked gas with quench water in countercurrent flow in said final stage; withdrawing cleaned and cooled cracked gas from said final stage; withdrawing remaining liquid quench oil from said first stage after said quench oil has contacted said cracked gas; passing at least a portion of said withdrawn quench oil to a cooling zone and thence recycling cooled withdrawn quench oil to said first stage; removing a second portion of said withdrawn quench oil from the quenching process; withdrawing remaining liquid second quench oil from said second sta e after said second quench 01! 1s contacted with said cracke gas; passing at least a portion of said withdrawn remaining liquid second quench oil to a cooling zone and thence recycling cooled second quench oil to the second stage; withdrawing a liquid from said final stage containing hydrocarbon, water, and a hydrocarbonwater emulsion; passing said withdrawn liquid to a separation zone wherein said liquid is separated into a hydrocarbon phase, a water phase, and a hydrocarbon-water emulsion phase; transferring the separated hydrocarbon-water emulsion phase from said separation zone to the first stage of the quenching zone at a point which is below the point at which the cracked gas contacts the quench oil; transferring at least a portion of said separated water phase to a cooling zone and thence to the final stage of the quenching zone; and transferring at least a portion of said separated hydrocarbon phase from said separation zone to the first stage of the quenching zone.

22. The process of claim 21 wherein the cracked gas entering the quenching zone contains particulate carbon and the hydrocarbon-water emulsion separated from the liquid phase withdrawn from said final stage contains particulate carbon.

i t i i 

2. The process of claim 1 wherein the pyrolytically cracked gas contains from about 0.001 to about 0.10 pounds of particulate carbon per pound of dry gas.
 3. The process of claim 1 wherein the pressure within the quenching zone is about 0.1 to about 10 atmospheres at the surface of the liquid.
 4. The process of claim 2 wherein the hydrocarbon-water emulsion contains about 0.0001 to about 0.2000 pounds of particulate carbon per pound of emulsion.
 5. The process of claim 1 wherein the pyrolytically cracked gas and the quench oil are contacted in countercurrent flow.
 6. The process of claim 1 wherein at least a portion of the quench oil remains in a liquid phase in the first stage of the quenching zone.
 7. The process of claim 6 wherein said remaining liquid quench oil is separated from the cracked gas after the quench oil contacts the cracked gas.
 8. The process of claim 7 wherein at least a portion of the separated liquid quench oil is recycled into the first stage of the quenching zone.
 9. The process of claim 7 wherein at least a portion of the separated liquid quench oil is cooled and then recycled to the first stage of the quenching zone.
 10. The process of claim 7 wherein the separated liquid quench oil contains particulate carbon.
 11. The process of claim 7 wherein at least a portion of the separated liquid oil is withdrawn from the quenching process thereby removing particulate carbon from the process.
 12. The process of claim 1 wherein the temperature of the cracked gas passing from the first stage of the quenching zone to the stage subsequent to the first stage is about 15* C. to about 500* C.
 13. The process of claim 1 wherein the temperature within the separation zone is about 10* C. to about 150* C.
 14. The process of claim 1 wherein the pressure within the separation zone is about 0.1 to about 10 atmospheres at the surface of the liquid.
 15. The process of claim 1 wherein a portion of the hydrocarbon phase separated in the separation zone is transferred to the first stage of the quenching zone and is contacted with the pyrolytically cracked gas.
 16. The process of claim 1 wherein a portion of the water phase separated in the separation zone is transferred to said subsequent stage and is contacted with the cracked gas.
 17. In the regenerative pyrolytic hydrocarbon cracking process for producing acetylene, e.g., the Wulff process, wherein the exhaust gases produced in the generation step of the regeneration process containing particulate carbon and hydrocarbons are scrubbed with a scrubbing liquid to remove particulate carbon and wherein a slurry of particulate carbon, hydrocarbons and scrubbing liquid is produced and wherein the pyrolytically cracked gas containing acetylene is quenched in a quenching process having a plurality of stages, the first stage of which comprises contacting the cracked gas with a quench oil; the improvement comprising in combination transferring said slurry of particulate carbon and scrubbing liquid to the first stage of the quenching process and contacting said slurry with the cracked gas in the first stage of the quenching process at a point which is below the point at which the cracked gas is contacted with the quench oil, thereby vaporizing at least a part of the scrubbing liquid such that the particulate carbon may be entrained in the quench oil.
 18. The process of claim 17 wherein the scrubbing liquid is water and wherein substantially all of the water is vaporized in the first stage of the quenching process.
 19. The process of claim 17 wherein the scrubbing liquid is a hydrocarbon.
 20. The process of claim 17 wherein the scrubbing liquid is a mixture of hydrocarbon and water and wherein substantially all of the water is vaporized in the first stage of the quenching process.
 21. In a process for quenching pyrolytically cracked gas containing alkenes and alkynes having two or more carbon atoms and wherein the cracked gas is cleaned and cooled in a quenching zone; the improvement comprising in combination passing said cracked gas to a quenching zone having three stages; contacting said cracked gas with quench oil in countercurrent flow in a first stage; passing said cracked gas from said first stage to a second stage; contacting said cracked gas with a second quench oil in countercurrent flow in a second or intermediate stage; maintaining the temperature, pressure and water concentration in said first and intermediate stages such that substantially no water vapor is condensed in said first and intermediate stages; passing said cracked gas from said second stage to a final stage; contacting said cracked gas with quench water in countercurrent flow in said final stage; withdrawing cleaned and cooled cracked gas from said final stage; withdrawing remaining liquid quench oil from said first stage after said quench oil has contacted said cracked gas; passing at least a portion of said withdrawn quench oil to a cooling zone and thence recycling cooled withdrawn quench oil to said first stage; removing a second portion of said withdrawn quench oil from the quenching process; withdrawing remaining liquid second quench oil from said second stage after said second quench oil is contacted with said cracked gas; passing at least a portion of said withdrawn remaining liquid second quench oil to a cooling zone and thence recycling cooled second quench oil to the second stage; withdrawing a liquid from said final stage containing hydrocarbon, water, and a hydrocarbon-water emulsion; passing said withdrawn liquid to a separation zone wherein said liquid is separated into a hydrocarbon phase, a water phase, and a hydrocarbon-water emulsion phase; transferring the separated hydrocarbon-water emulsion phase from said separation zone to the first stage of the quenching zone at a point which is below the point at which the cracked gas contacts the quench oil; transferring at least a portion of said separated water phase to a cooling zone and thence to the final stage of the quenching zone; and transferring at least a portion of said separated hydrocarbon phase from said separation zone to the first stage of the quenching zone.
 22. The process of claim 21 wherein the cracked gas entering the quenching zone contains particulate carbon and the hydrocarbon-water emulsioN separated from the liquid phase withdrawn from said final stage contains particulate carbon. 